COrecovery unit and COrecovery method

A CO2 recovery unit and a CO2 recovery method capable of having an excellent CO2 absorption rate and saving energy are provided. A CO2 recovery unit of the invention includes: a CO2 absorber which includes an upper CO2 absorption unit obtaining a CO2 absorbent by causing a flue gas containing CO2 to contact a CO2 absorbent and a lower CO2 absorption unit obtaining a CO2 absorbent by causing the CO2 absorbent to contact a flue gas containing CO2; a CO2 absorbent regenerator which obtains the CO2 absorbent by heating the CO2 absorbent a thermometer which measures a temperature of the CO2 absorbent supplied from the CO2 absorber to the CO2 absorbent regenerator; and a control device which controls a temperature of the CO2 absorbent supplied to the lower CO2 absorption unit based on the temperature of the CO2 absorbent measured by the thermometer.

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Description
FIELD

The present invention relates to a CO2 recovery unit and a CO2 recovery method and particularly to a CO2 recovery unit and a CO2 recovery method which recover CO2 in a gas to be treated by using a CO2 absorbent.

BACKGROUND

Hitherto, there has been proposed a direct-reduced iron reduction system including an acid gas removing device for removing an acid element in a reducing furnace flue gas corresponding to a synthetic gas discharged from a direct reducing furnace (for example, see Patent Literature 1). In this direct-reduced iron reduction system, the reducing furnace flue gas having a high CO2 partial pressure (for example, 50 kPa to 200 kPa) and discharged from the direct reducing furnace is caused to contact an acid gas absorbent in an acid gas element-absorber so that an acid gas element in the reducing furnace flue gas is removed therefrom. The acid gas absorbent having the acid gas element absorbed thereto is heated in a regenerator to discharge the acid gas element in the acid gas absorbent therefrom so that the acid gas absorbent is regenerated. Further, there is also proposed an acid gas removing facility which removes an acid element contained in a natural gas (for example, see Non Patent-Literature 1).

CITATION LIST Patent Literature

  • Patent Literature 1: Japanese Laid-open Patent Publication No. 2013-108109

Non Patent Literature

  • Non Patent Literature 1: Liquefying Plant Essential Knowledge for Understanding LNG Business (oilgas-info.jogmec.go.jp/pdf/0/598/200503_001a.pdf)

SUMMARY Technical Problem

Incidentally, a CO2 recovery unit which recovers CO2 in a combustion flue gas having a relatively low CO2 partial pressure (for example, 10 kPa to 15 kPa) and discharged from a boiler or the like by using a CO2 absorbent is used in a thermal power station or the like. Likewise, various methods have been examined in order to save energy. In recent years, it is desirable to develop a technology capable of having a small CO2 recovery heat amount involved with a steam consumption amount and realizing energy saving even when CO2 in a synthetic gas having a relatively high CO2 partial pressure is recovered by a CO2 absorbent or CO2 in a natural gas (a methane gas) containing CO2 is recovered by a CO2 absorbent.

This invention is contrived in view of such circumstances and an object of the invention is to provide a CO2 recovery unit and a CO2 recovery method capable of both having an excellent CO2 absorption rate and saving energy.

Solution to Problem

A CO2 recovery unit according to the present invention comprising: a CO2 absorber which includes a first CO2 absorption unit obtaining a first CO2 absorbent by causing a CO2 containing gas to be treated to contact a CO2 absorbent so that CO2 contained in the gas to be treated is absorbed to the CO2 absorbent and a second CO2 absorption unit obtaining a second CO2 absorbent by causing the first CO2 absorbent to contact a CO2 containing gas to be treated so that CO2 contained in the gas to be treated is absorbed to the first CO2 absorbent; a CO2 absorbent regenerator which regenerates a CO2 absorbent by heating the second CO2 absorbent so that CO2 is discharged from the second CO2 absorbent; a temperature measurement device which measures a temperature of the second CO2 absorbent supplied from the CO2 absorber to the CO2 absorbent regenerator; and a control device which controls a temperature of the first CO2 absorbent supplied to the second CO2 absorption unit based on the temperature of the second CO2 absorbent measured by the temperature measurement device.

According to this configuration, since the temperature of the first CO2 absorbent supplied to the second CO2 absorption unit is controlled based on the temperature of the second CO2 absorbent supplied to the CO2 absorbent regenerator, the CO2 absorption rate of the CO2 absorbent in the second CO2 absorption unit can be increased. Accordingly, the CO2 recovery unit can have an excellent CO2 absorption rate and save energy even when a synthetic gas having a high CO2 partial pressure in a gas to be treated is treated. Here, the absorption rate indicates a CO2 absorption molar amount per 1 mol of an absorbent.

In the CO2 recovery unit according to present invention, it is preferable that the control device controls the temperature of the first CO2 absorbent supplied to the second CO2 absorption unit so that the temperature is equal to or higher than 50° C. and equal to or lower than 60° C. With this configuration, since the CO2 recovery unit controls the temperature of the first CO2 absorbent supplied to the second CO2 absorption unit within an appropriate range, the CO2 absorption rate of the gas to be treated in the second CO2 absorption unit is further improved and the circulation amount of the CO2 absorbent can be decreased in accordance with the improved CO2 absorption rate. Accordingly, the amount of steam necessary to regenerate the CO2 absorbent can be decreased. With this configuration, the temperature of the CO2 absorbent supplied to the CO2 absorbent regenerator can be appropriately increased and thus an effect of decreasing a steam consumption amount is expected.

In the CO2 recovery unit according to present invention, it is preferable that a CO2 partial pressure of the CO2 containing gas to be treated is 50 kPa or more. With this configuration, since the CO2 recovery unit controls the CO2 partial pressure in the gas to be treated within an appropriate range, the CO2 absorption rate using the first CO2 absorbent in the second CO2 absorption unit is further improved.

In the CO2 recovery unit according to present invention, it is preferable that a ratio (the first CO2 absorption unit:the second CO2 absorption unit) between a filling material charging height in the first CO2 absorption unit and a filling material charging height in the second CO2 absorption unit is equal to or larger than 1:3 and equal to or smaller than 3:1. With this configuration, since the CO2 absorption rate in the gas to be treated using the CO2 absorbent is further improved, energy can be saved.

A CO2 recovery method according to the present invention comprising: obtaining a first CO2 absorbent by causing a CO2 containing gas to be treated to contact a CO2 absorbent in a first CO2 absorption unit of a CO2 absorber so that CO2 contained in the gas to be treated is absorbed to the CO2 absorbent and obtaining a second CO2 absorbent by causing the first CO2 absorbent to contact the CO2 containing gas to be treated in a second CO2 absorption unit of the CO2 absorber so that CO2 contained in the gas to be treated is absorbed to the first CO2 absorbent; regenerating a CO2 absorbent by heating the second CO2 absorbent in a CO2 absorbent regenerator so that CO2 is discharged from the CO2 absorbent; and measuring a temperature of the second CO2 absorbent supplied from the CO2 absorber to the CO2 absorbent regenerator and controlling a temperature of the first CO2 absorbent supplied to the second CO2 absorption unit based on the measured temperature of the second CO2 absorbent.

According to this method, since the temperature of the first CO2 absorbent supplied to the second CO2 absorption unit is controlled based on the temperature of the second CO2 absorbent supplied to the CO2 absorbent regenerator, the CO2 absorption rate of the CO2 absorbent in the second CO2 absorption unit can be increased. Accordingly, the CO2 recovery method can have an excellent CO2 absorption rate and save energy even when a synthetic gas having a high CO2 partial pressure in a gas to be treated is treated.

In the CO2 recovery method according to present invention, it is preferable that the temperature of the first CO2 absorbent supplied to the second CO2 absorption unit is controlled so that the temperature is equal to or higher than 50° C. and equal to or lower than 60° C. With this method, since the CO2 recovery unit controls the temperature of the first CO2 absorbent supplied to the second CO2 absorption unit within an appropriate range, the CO2 absorption rate of the gas to be treated in the second CO2 absorption unit is further improved and the circulation amount of the CO2 absorbent can be decreased in accordance with the improved CO2 absorption rate. Accordingly, the amount of steam necessary to regenerate the CO2 absorbent can be decreased. With this configuration, the temperature of the CO2 absorbent supplied to the CO2 absorbent regenerator can be appropriately increased and thus an effect of decreasing a steam consumption amount is expected.

In the CO2 recovery method according to present invention, it is preferable that a CO2 partial pressure of the CO2 containing gas to be treated is 50 kPa or more. With this method, since the CO2 recovery method controls the CO2 partial pressure in the gas to be treated within an appropriate range, the CO2 absorption rate in the gas to be treated using the first CO2 absorbent in the second CO2 absorption unit is further improved.

In the CO2 recovery method according to present invention, it is preferable that a ratio (the first CO2 absorption unit:the second CO2 absorption unit) between a filling material charging height in the first CO2 absorption unit and a filling material charging height in the second CO2 absorption unit is equal to or larger than 1:3 and equal to or smaller than 3:1. With this method, since the CO2 absorption rate in the gas to be treated using the CO2 absorbent is further improved, energy can be saved.

Advantageous Effects of Invention

According to the invention, it is possible to realize a CO2 recovery unit and a CO2 recovery method both having an excellent CO2 absorption rate and realizing energy saving.

BRIEF DESCRIPTION OF DRAWINGS

FIG. 1 is a schematic diagram illustrating a CO2 recovery unit according to an embodiment of the invention.

FIG. 2 is a diagram illustrating a relation between a temperature of a CO2 absorbent (a semi-rich solution) supplied to a lower CO2 absorption unit and a ratio of a CO2 absorption rate of a rich solution.

FIG. 3 is a diagram illustrating a relation between a temperature of a CO2 absorbent (a semi-rich solution) supplied to a lower CO2 absorption unit and a ratio of a heat amount necessary to regenerate the CO2 absorbent.

FIG. 4 is a diagram illustrating a relation between a temperature of a CO2 absorbent (a semi-rich solution) supplied to a lower CO2 absorption unit and a temperature of a CO2 absorbent (a rich solution) supplied to a CO2 absorbent regenerator.

FIG. 5 is a diagram illustrating a relation of filling material charging height ratios of a lower CO2 absorption unit and an upper CO2 absorption unit of a CO2 absorber with respect to a ratio of a CO2 absorption rate of a rich solution.

 DESCRIPTION OF EMBODIMENTS

The present inventors have paid attention to a conventional CO2 recovery unit which recovers CO2 from a gas having a relatively low CO2 partial pressure (for example, 10 kPa to 15 kPa) such as a combustion flue gas discharged from a boiler of a thermal power station and does not recover CO2 from a synthetic gas having a relatively high CO2 partial pressure (for example, 50 kPa to 200 kPa) and discharged from a direct reducing furnace. Then, the present inventors have found that a CO2 recovery unit and a CO2 recovery method capable of both having an excellent CO2 absorption rate and saving energy are obtained by a configuration in which a CO2 absorber is provided with a plurality of CO2 absorption units and a temperature of a CO2 absorbent supplied to the plurality of CO2 absorption units is controlled based on a temperature of a CO2 absorbent supplied to a CO2 absorbent regenerator when CO2 is recovered from a synthetic gas having a relatively high CO2 partial pressure, whereby the invention is obtained.

Hereinafter, an embodiment of the invention will be described in detail with reference to the accompanying drawings. The invention is not limited to the embodiments below and can be appropriately modified. Further, the components of the CO2 recovery unit according to the embodiments below can be appropriately combined with one another.

FIG. 1 is a schematic diagram illustrating a CO2 recovery unit according to an embodiment of the invention. As illustrated in FIG. 1, a CO2 recovery unit 1 is an apparatus which recovers CO2 in a reducing furnace flue gas (a gas to be treated) 11A, corresponding to a synthetic gas discharged from a direct reducing furnace, in the form of a high-concentration CO2 gas. The CO2 recovery unit 1 includes a cooling tower 12 which cools a flue gas 11A containing CO2 discharged from a direct reducing furnace, a CO2 absorber 14 which is provided at a rear stage of the cooling tower 12 and causes the cooled flue gas 11A to contact a CO2 absorbent 13 so that CO2 in the flue gas 11A is absorbed to the CO2 absorbent 13 to be removed from the flue gas, and a CO2 absorbent regenerator 15 which is provided at a rear stage of the CO2 absorber 14 and discharges CO2 from a CO2 absorbent 13C having CO2 absorbed thereto to regenerate the CO2 absorbent 13.

In the CO2 recovery unit 1, the CO2 absorbent 13 is circulated between the CO2 absorber 14 and the CO2 absorbent regenerator 15. The CO2 absorbent 13 (a lean solution) is supplied as the CO2 absorbent 13C having CO2 absorbed thereto (a rich solution) in the CO2 absorber 14 to the CO2 absorbent regenerator 15. Further, CO2 is removed from the CO2 absorbent 13C (the rich solution) by the CO2 absorbent regenerator 15 and a resultant gas is supplied as the regenerated CO2 absorbent 13 (the lean solution) to the CO2 absorber 14.

The cooling tower 12 includes a cooling unit 121 which cools the flue gas 11A. Further, a circulation line L1 is provided between a bottom portion of the cooling tower 12 and a top portion of the cooling unit 121. The circulation line L1 is provided with a heat exchanger 122 which cools cooling water W1, a circulation pump 123 which circulates the cooling water W1 in the direction line L1, and an adjustment valve 124 which adjusts the amount of a waste liquid separated as a liquid from the circulation line L1 and discharged therefrom.

In the cooling unit 121, the flue gas 11A is cooled by a counterflow contact between the flue gas 11A and the cooling water W1 and thus a cooled flue gas 11B is obtained. The heat exchanger 122 cools the cooling water W1 which is heated by exchanging heat with the flue gas 11A. The circulation pump 123 supplies the cooling water W1 flowing down to the bottom portion of the cooling tower 12 through the heat exchanger 122 to a top portion of the cooling unit 121. In the cooling tower 12, when the amount of moisture in the flue gas 11A is small, a liquid level of the cooling tower 12 decreases and thus water is supplied from a tower top portion. Further, when the amount of the moisture in the flue gas 11A is large, the liquid level of the cooling tower 12 increases and thus a part of the cooling water W1 circulated in the circulation line L1 is separated as waste liquid.

The CO2 absorber 14 includes a CO2 absorption unit 141 which is provided in a lower portion of the CO2 absorber 14 and to which the CO2 absorbent 13 and the flue gas 11B cooled by the cooling tower 12 are supplied, and a water washing unit 142 which is provided in an upper portion of the CO2 absorber 14.

The CO2 absorption unit 141 includes a lower CO2 absorption unit (a second CO2 absorption unit) 141A which is provided in a lower portion of the CO2 absorption unit 141 and an upper CO2 absorption unit 141B (a first CO2 absorption unit) which is provided in an upper portion of the CO2 absorption unit 141. A filling material is charged into the lower CO2 absorption unit 141A at a charging height H1. A filling material is charged into the upper CO2 absorption unit 141B at a charging height H2. The CO2 absorbent 13 which is regenerated by the CO2 absorbent regenerator 15 is supplied to the upper CO2 absorption unit 141B. A CO2 absorbent 13B which absorbs CO2 in a flue gas 11C by the upper CO2 absorption unit 141B is supplied to the lower CO2 absorption unit (the second CO2 absorption unit) 141A.

A liquid storage unit 143A, which stores a CO2 absorbent (a first CO2 absorbent) 13A flowing down from the upper CO2 absorption unit 141B and staying at a lower portion of the upper CO2 absorption unit 141B, and a chimney tray 143B are provided between the lower CO2 absorption unit 141A and the upper CO2 absorption unit 141B. The liquid storage unit 143A is provided with an extraction line L11 which extracts the CO2 absorbent 13A stored in the liquid storage unit 143A from the CO2 absorber 14 and supplies the liquid to the lower CO2 absorption unit 141A.

The extraction line L11 is provided with a heat exchanger 24 which cools the CO2 absorbent 13A to obtain the cooled CO2 absorbent 13B and a pump 25 which supplies the CO2 absorbent 13A as the CO2 absorbent 13B to the lower CO2 absorption unit 141A. The heat exchanger 24 is configured to adjust a refrigerant supply amount by a control device 101. Further, the pump 25 is configured to adjust the amount of the CO2 absorbent 13B supplied to the lower CO2 absorption unit 141A by the control device 101. The control device 101 can be realized by, for example, a general or dedicated computer such as a CPU (Central Processing Unit), a ROM (Read Only Memory)/and a RAM (Random Access Memory) and a program operated on this computer.

A bottom portion of the water washing unit 142 is provided with a liquid storage unit 144A which stores washing water W2 for washing a flue gas 11D obtained by removing CO2 therefrom in the flue gas 11C. A circulation line L2 which supplies the washing water W2 containing the CO2 absorbent 13 recovered by the liquid storage unit 144A from a top portion of the water washing unit 142 so that the washing water is circulated is provided between the liquid storage unit 144A and the water washing unit 142. The circulation line L2 is provided with a heat exchanger 21 which cools the washing water W2 and a circulation pump 22 which circulates the washing water W2 containing the CO2 absorbent 13 recovered by the liquid storage unit 144A through the heat exchanger 21 so that the washing water is circulated in the circulation line L2. Further, the circulation line L2 is provided with an extraction line L3 which extracts a part (washing water W3) of the washing water W2 and supplies the water to the CO2 absorbent 13 (the lean solution). The extraction line L3 is provided with an adjustment valve 23 which adjusts the amount of the washing water W3 supplied to the CO2 absorbent 13.

In the CO2 absorption unit 141, a counterflow contact between the flue gas 11A containing CO2 by the upper CO2 absorption unit 141B and the CO2 absorbent 13 containing alkanolamine occurs. Accordingly, CO2 in the flue gas 11C is absorbed to the CO2 absorbent 13 by a chemical reaction expressed in the following formula. As a result, CO2 in the flue gas 11C is removed so that the flue gas 11C becomes the flue gas 11D obtained by removing CO2 therefrom and the CO2 absorbent 13 becomes the CO2 absorbent 13A. Then, in the lower CO2 absorption unit 141A, a counterflow contact between the flue gas 11B containing CO2 and the CO2 absorbent 13B having CO2 absorbed thereto occurs. Accordingly, CO2 in the flue gas 11B is absorbed to the CO2 absorbent 13B by the chemical reaction expressed in the following formula. As a result, CO2 in the flue gas 11B is removed so that the flue gas 11B becomes the flue gas 11C of which a CO2 concentration is decreased and the CO2 absorbent 13B becomes the CO2 absorbent 13C. In this way, when the flue gas 11B containing CO2 passes through the CO2 absorption unit 141, the flue gas 11D obtained by removing CO2 therefrom is obtained. Further, the CO2 absorbent 13 absorbs CO2 to become the CO2 absorbent 13B (the semi-rich solution) in the upper CO2 absorption unit 141B and the CO2 absorbent 13B further absorbs CO2 to become the CO2 absorbent 13C (the rich solution) in the lower CO2 absorption unit 141A.
R—NH2+H2O+CO2→R—NH3HCO3

In the water washing unit 142, the flue gas 11D obtained by removing CO2 therefrom after passing through the upper CO2 absorption unit 141B rises through a chimney tray 144B. Then, a gas-liquid contact occurs between the flue gas 11D and the washing water W2 supplied from the top portion of the water washing unit 142 so that a flue gas 11B is obtained by recovering the CO2 absorbent 13 accompanied by the flue gas 11D through circulating and washing processes. After mist in the flue gas 11E is trapped by a mist eliminator 145, the flue gas is discharged to the outside from a tower top portion 14a of the CO2 absorber 14.

A rich solution supply pipe 50 which supplies the CO2 absorbent 13C having CO2 absorbed thereto (the rich solution) in the CO2 absorber 14 to an upper portion of the CO2 absorbent regenerator 15 is provided between a tower bottom portion 14b of the CO2 absorber 14 and the upper portion of the CO2 absorbent regenerator 15. The rich solution supply pipe 50 is provided with a thermometer (a temperature measurement device) 102 which measures a temperature of the CO2 absorbent 13C, a rich solution pump 51 which supplies the CO2 absorbent 13C having CO2 absorbed thereto in the CO2 absorber 14 to the CO2 absorbent regenerator 15, and a rich-lean solution heat exchanger 52 which heats the CO2 absorbent 13C by the CO2 absorbent 13 (the lean solution) heated by the CO2 absorbent regenerator 15 to remove CO2 therefrom. The control device 101 adjusts the amount of a refrigerant supplied to the heat exchanger 24 based on a temperature of the CO2 absorbent 13C measured by the thermometer 102 and controls the amount of the CO2 absorbent 13B supplied to the lower CO2 absorption unit 141A by the pump 25. Additionally, the thermometer 102 may be provided at a position where the CO2 absorbent 13B supplied to the lower CO2 absorption unit 141A can be controlled by the control device 101. For example, the thermometer may be provided at a rear stage of the heat exchanger 24 of the extraction line L11.

A CO2 absorbent supply unit 151 to which the CO2 absorbent 13C having CO2 absorbed thereto is supplied is provided at a enter portion of the CO2 absorbent regenerator 15. A tower bottom portion 15b of the CO2 absorbent regenerator 15 is provided with a circulation line L4 which circulates the CO2 absorbent 13C flowing down to the tower bottom portion. The circulation line L4 is provided with a regenerating heater 31 which heats the CO2 absorbent 13 by saturated steam S, an adjustment valve 32 which supplies the saturated steam S to the regenerating heater 31, and a circulation pump 33 which supplies the CO2 absorbent 13 of a tower bottom portion of the CO2 absorbent regenerator 15 to a lower portion of the CO2 absorbent supply unit 151 of the CO2 absorbent regenerator 15 through the regenerating heater 31.

A tower top portion 15a of the CO2 absorbent regenerator 15 is provided with a gas discharge line L5 which discharges a CO2 gas 41 accompanying steam. The gas discharge line L5 is provided with a condenser 42 which condenses moisture in the CO2 gas 41 and a separation drum 43 which separates water W5 condensed by the CO2 gas 41. A CO2 gas 44 from which the condensed water W5 is separated is discharged to the outside from the upper portion of the separation drum 43. A condensed water line L6 which supplies the condensed water W5 separated in the separation drum 43 to an upper portion of the CO2 absorbent regenerator 15 is provided between the bottom portion of the separation drum 43 and the upper portion of the CO2 absorbent regenerator 15. The condensed water line L6 is provided with a condensed water circulation pump 45 which supplies the condensed water W5 separated in the separation drum 43 to the upper portion of the CO2 absorbent regenerator 15. An adjustment valve 46 which controls the amount of the condensed water W5 supplied to the CO2 absorbent regenerator 15 is provided between the condensed water circulation pump 45 and the CO2 absorbent regenerator 15. Further, a re-circulation line L12 which divides a part of the condensed water W5 supplied to the CO2 absorbent regenerator 15 and re-circulates the condensed water W5 supplied to the water washing unit 142 of the CO2 absorber 14 is provided between the condensed water circulation pump 45 and the circulation line L2. The re-circulation line L12 is provided with an adjustment valve 47 which adjusts the amount of the condensed water W5 supplied to the water washing unit 142.

Further, the tower bottom portion of the CO2 absorbent regenerator 15 and the upper portion of the CO2 absorption unit 141 of the CO2 absorber 14 are provided with a lean solution supply pipe 53 which supplies the CO2 absorbent 13 (the lean solution) of the tower bottom portion of the CO2 absorbent regenerator 15 to the upper portion of the CO2 absorption unit 141. The lean solution supply pipe 53 is provided with the rich-lean solution heat exchanger 52 which heats the CO2 absorbent 13C having CO2 absorbed thereto (the rich solution) by the CO2 absorbent 13 (the lean solution) heated by the steam in the CO2 absorbent regenerator 15 so that CO2 is removed therefrom, a lean solution pump 54 which supplies the CO2 absorbent 13 of the tower bottom portion of the CO2 absorbent regenerator 15 to the upper portion of the CO2 absorption unit 141, and a cooling unit 55 which cools the CO2 absorbent 13 (the lean solution) to a predetermined temperature.

Next, a relation between a CO2 absorption rate and a temperature of the CO2 absorbent 13B supplied to the lower CO2 absorption unit 141A of the CO2 absorber 14 in the CO2 recovery unit 1 according to the embodiment will be described with reference to FIG. 2. FIG. 2 is a diagram illustrating a relation between the temperature of the CO2 absorbent 13B (the semi-rich solution) supplied to the lower CO2 absorption unit and a ratio of the CO2 absorption rate of the rich solution. Additionally, in FIG. 2, a horizontal axis indicates the temperature of the CO2 absorbent 13B and a vertical axis indicates the ratio of the CO2 absorption rate of the rich solution. Further, in FIG. 2, a case where a flue gas having a low CO2 partial pressure (for example, about 10 kPa) such as a combustion flue gas discharged from a boiler is used is indicated by a dotted line and a case where a flue gas having a high CO2 partial pressure (for example, about 60 kPa) such as a synthetic gas discharged from a direct reducing furnace is used is indicated by a solid line. Additionally, a plot indicates an analysis value. Further, in FIG. 2, the flue gas having a low CO2 partial pressure and the flue gas having a high CO2 partial pressure are displayed on the same axes at a ratio in which a maximal value of the absorption rate is 1 in a temperature range equal to or higher than 40° C. and equal to or lower than 70° C., but have different maximal values of the absorption rates.

As indicated by the dotted line of FIG. 2, when the flue gas having a low CO2 partial pressure is used, the CO2 absorption rate of the CO2 absorbent 13B increases in accordance with a decrease in temperature. For this reason, it is desirable to decrease a temperature of the CO2 absorbent 13B in order to efficiently recover CO2 in the flue gas having a low CO2 partial pressure.

Meanwhile, when the flue gas having a high CO2 partial pressure is used as indicated by the solid line of FIG. 2, the CO2 absorption rate has a different tendency from the case where the flue gas having a low CO2 partial pressure is used. When the flue gas having a high CO2 partial pressure is used, the CO2 absorption rate becomes maximal at about 55° C., and the CO2 absorption rate decreases as the temperature falls from 55° C. However, in the embodiment, compared with the case where the flue gas having a low CO2 partial pressure is used, it is possible to improve the CO2 absorption rate in the lower CO2 absorption unit 141A by controlling the temperature of the CO2 absorbent 13B supplied to the lower CO2 absorption unit 141A in an operation state and to decrease the heat amount of the CO2 absorbent 13C in the CO2 absorbent regenerator 15 by decreasing the circulation amount of the CO2 absorbent. Accordingly, energy saving is realized.

As illustrated in FIG. 2, in the CO2 recovery unit 1 according to the embodiment, it is desirable to control the temperature of the CO2 absorbent 13B supplied to the lower CO2 absorption unit 141A in a range equal to or higher than 50° C. and equal to or lower than 60° C. by the control device 101. Accordingly, the CO2 recovery unit 1 can set the temperature of the CO2 absorbent 13B supplied to the lower CO2 absorption unit 141A within an appropriate range. For this reason, it is possible to further improve the CO2 absorption rate of the flue gas 11A by the CO2 absorbent 13B in the lower CO2 absorption unit 141A and to decrease the circulation amount of the CO2 absorbent 13B in accordance with the improved CO2 absorption rate. Thus, it is possible to decrease the amount of the saturated steam S consumed to regenerate the CO2 absorbent 13C. Further, the CO2 recovery unit 1 can set the temperature of the CO2 absorbent 13C supplied to the CO2 absorbent regenerator 15 to an appropriately high temperature and thus an effect of decreasing a steam consumption amount is obtained.

Additionally, in the embodiment, the CO2 partial pressure of the flue gas 11B is desirably equal to or higher than 50 kPa and equal to or lower than 200 kPa. When the CO2 partial pressure is equal to or higher than 50 kPa, the CO2 absorption rate of the lower CO2 absorption unit 141A has a different tendency when the CO2 partial pressure is low (for example, about 10 kPa) as indicated by the solid line of FIG. 2. Further, when the CO2 partial pressure is equal to or lower than 200 kPa, the amount of CO2 in the flue gas 11B can be sufficiently decreased by the CO2 absorber 14. From the viewpoint of improving the above-described operations and effects, the CO2 partial pressure of the flue gas 11B is more desirably 55 kPa or more, further desirably 60 kPa or more, more desirably 150 kPa or less, and further desirably 100 kPa or less. When the above-described fact is taken into consideration, the CO2 partial pressure of the flue gas 11B is more desirably equal to or higher than 55 kPa and equal to or lower than 150 kPa and further desirably equal to or higher than 60 kPa and equal to or lower than 100 kPa.

Next, a relation between the temperature of the CO2 absorbent 13B supplied to the lower CO2 absorption unit 141A in the CO2 recovery unit 1 according to the embodiment and the heat amount necessary to regenerate the CO2 absorbent 13 in the CO2 absorbent regenerator 15 will be described with reference to FIG. 3. FIG. 3 is a diagram illustrating a relation between the temperature of the CO2 absorbent 13B (the semi-rich solution) supplied to the lower CO2 absorption unit 141A and a ratio of the heat amount necessary to regenerate the CO2 absorbent 13. Further, in FIG. 3, a horizontal axis indicates the temperature of the CO2 absorbent 13B and a vertical axis indicates the ratio of the heat amount necessary to regenerate CO2. Further, in FIG. 3, the flue gas having a high CO2 partial pressure is displayed as a ratio in which a minimal value of the heat amount necessary to regenerate the CO2 absorbent 13B is 1 in a temperature range equal to or higher than 40° C. and equal to or lower than 70° C. Additionally, a plot indicates an analysis value.

As illustrated in FIG. 3, when the flue gas having a high CO2 partial pressure is used, the heat amount necessary to regenerate the CO2 absorbent 13B in the CO2 absorbent regenerator 15 becomes minimal at about 55° C. and the heat amount necessary to regenerate the CO2 absorbent 13C increases as the temperature falls from 55° C. Thus, in the embodiment, as illustrated in FIG. 2, when the temperature of the CO2 absorbent 13B supplied to the lower CO2 absorption unit 141A is set to a range in which the CO2 absorption rate of the flue gas 11A using the CO2 absorbent 13B of the lower CO2 absorption unit 141A is high, it is possible to decrease the amount of the saturated steam S consumed to regenerate the CO2 absorbent 13C. This is because the circulation amount of the CO2 absorbent 13 can be decreased in accordance with improvement in absorption rate.

FIG. 4 is a diagram illustrating a relation between the temperature of the CO2 absorbent 13B (the semi-rich solution) supplied to the lower CO2 absorption unit 141A and the temperature of the CO2 absorbent 13C (the rich solution) supplied to the CO2 absorbent regenerator 15. Further, in FIG. 4, a vertical axis indicates the temperature of the CO2 absorbent 13C supplied to the CO2 absorbent regenerator 15 and a horizontal axis indicates the temperature of the CO2 absorbent 13B supplied to the lower CO2 absorption unit 141A.

As illustrated in FIG. 4, in the embodiment, there is a direct proportional relation between the temperature of the CO2 absorbent 13B supplied to the lower CO2 absorption unit 141A and the temperature of the CO2 absorbent 13C supplied to the CO2 absorbent regenerator 15. Thus, when the control device 101 controls the amount of the refrigerant supplied to the heat exchanger 24 and the amount of the CO2 absorbent 13B supplied to the lower CO2 absorption unit 141A by the pump 25 so that the temperature of the CO2 absorbent 13C supplied to the CO2 absorbent regenerator 15 is measured by the thermometer 102 and the measured temperature falls within a predetermined range (for example, a range equal to or higher than 62° C. and equal to or lower than 67° C.), it is possible to control the CO2 absorbent 13B of the lower CO2 absorption unit 141A at a desired temperature. Accordingly, it is possible to obtain a high CO2 absorption rate and to decrease a heat amount necessary to heat the CO2 absorbent 13C in the CO2 absorbent regenerator 15.

FIG. 5 is a diagram illustrating a relation of filling material charging height ratios H1 and H2 of the lower CO2 absorption unit and the upper CO2 absorption unit of the CO2 absorber with respect to a ratio of the CO2 absorption rate of the rich solution. Additionally, in FIG. 5, a case where the filling material charging height ratios (the upper CO2 absorption unit 141B:the lower CO2 absorption unit 141A) H1 and H2 of the lower CO2 absorption unit 141A and the upper CO2 absorption unit 141B are changed in a range of 1:3 to 3:1 is displayed at a ratio in which a maximal value of the CO2 absorption rate is 1.

As illustrated in FIG. 5, in the embodiment, when the filling material charging height ratios of the lower CO2 absorption unit 141A and the upper CO2 absorption unit 141B are changed, the CO2 absorption rate changes. For this reason, in the embodiment, it is desirable that the charging height ratio (the upper CO2 absorption unit 141B:the lower CO2 absorption unit 141A) between the charging height of the filling material the filling material H2 in the upper CO2 absorption unit 141B and the charging height of the filling material H1 in the lower CO2 absorption unit 141A be equal to or larger than 1:3 and equal to or smaller than 3:1. Accordingly, since the absorption efficiency for CO2 in the flue gas 11A of the upper CO2 absorption unit 141B and the absorption efficiency for CO2 in the flue gas 11A of the lower CO2 absorption unit 141A are respectively improved, it is possible to further improve a CO2 absorption rate and to save energy. As the charging height ratio, 1:1 is more desirable from the viewpoint of further improving the above-described operations and effects.

Next, an overall operation of the CO2 recovery unit 1 according to the embodiment will be described. The flue gas 11A such as a synthetic gas containing CO2 discharged from the direct reducing furnace is introduced into the cooling tower 12 and is cooled by a counterflow contact with respect to the cooling water W1 to become the flue gas 11B. The cooled flue gas 11B is introduced into the CO2 absorber 14 through a flue gas duct 16 and a flow rate of the flue gas 11B introduced into the CO2 absorber 14 is measured. A counterflow contact occurs between the flue gas 11B introduced into the CO2 absorber 14 and the CO2 absorbent 13 containing alkanolamine in the lower CO2 absorption unit 141A and the upper CO2 absorption unit 141B of the CO2 absorption unit 141 so that CO2 in the flue gas 11B is absorbed to the CO2 absorbent 13 and the flue gas 11D is obtained by removing CO2 therefrom.

The flue gas 11D obtained by removing CO2 therefrom rises through the chimney tray 144B and causes a gas-liquid contact with respect to the washing water W2 supplied from the top portion of the water washing unit 142 so that the flue gas 11E is obtained by recovering the CO2 absorbent 13 accompanied by the flue gas 11D through a circulating and washing process. Mist is the flue gas 11E is trapped by the mist eliminator 145 and the flue gas is discharged to the outside from the tower top portion 14a of the CO2 absorber 14.

The CO2 absorbent 13C having CO2 absorbed thereto in the CO2 absorber 14 exchanges heat with the CO2 absorbent 13 (the lean solution) in the rich-lean solution heat exchanger 52 through the rich solution supply pipe 50 and is supplied to the upper portion of the CO2 absorbent regenerator 15 by the rich solution pump 51. Here, in the embodiment, the CO2 absorbent 13C flowing in the rich solution supply pipe 50 is measured at all times by the thermometer 102 and the measured temperature of the CO2 absorbent 13C is transmitted to the control device 101. The control device 101 adjusts the amount of the refrigerant supplied to the heat exchanger 24 and the amount of the CO2 absorbent 13B supplied to the lower CO2 absorption unit 141A by the pump 25 so that the temperature of the CO2 absorbent 13C measured by the thermometer 102 falls within a predetermined range.

CO2 is removed from the CO2 absorbent 13C supplied to the CO2 absorbent regenerator 15 while the CO2 absorbent 13C flows down to the tower bottom portion through the CO2 absorbent supply unit 151 and thus a semi-lean solution is obtained. This semi-lean solution is circulated in the circulation line L4 by the circulation pump 33 and is heated by the saturated steam S in the regenerating heater 31 so that the CO2 absorbent 13 (the lean solution) is obtained. The heated saturated steam S becomes the steam condensed water W4. The CO2 gas 41 removed from the CO2 absorbent 13 passes through the condenser 42 so that moisture is removed therefrom and is discharged as the CO2 gas 44, from which the condensed water W5 is separated, to the outside from the upper portion of the separation drum 43, The separated condensed water W5 is supplied to the CO2 absorbent regenerator 15 and a part of the water is divided so that the water is supplied to the water washing unit 142 of the CO2 absorber 14 through the re-circulation line L12.

The CO2 absorbent 13 (the lean solution) of the tower bottom portion 15b of the CO2 absorbent regenerator 15 exchanges heat with the CO2 absorbent 13C (the rich solution) by the rich-lean solution heat exchanger 52 through the lean solution supply pipe 53 and is supplied to the upper portion of the CO2 absorption unit 141 of the CO2 absorber 14 by the lean solution pump 54. The CO2 absorbent 13 supplied to the CO2 absorption unit 141 absorbs CO2 of the flue gas 11A in the upper CO2 absorption unit 141B to become the CO2 absorbent (the semi-rich solution) 13A and is extracted from the lower portion of the upper CO2 absorption unit 141B to the extraction line L11. The extracted CO2 absorbent 13A is cooled to a predetermined temperature range by the heat exchanger 24 to become the CO2 absorbent (the semi-rich solution) 13B and is supplied to the lower CO2 absorption unit 141A by the pump 25 to absorb CO2 in the flue gas 11B by the lower CO2 absorption unit 141A so that the CO2 absorbent (the rich solution) 13C is obtained. The CO2 absorbent (the rich solution) 13C is extracted from the tower bottom portion 14b of the CO2 absorber 14 and is supplied to the CO2 absorbent regenerator 15.

As described above, according to the embodiment, since the temperature of the CO2 absorbent 13B supplied to the lower CO2 absorption unit 141A is controlled based on the temperature of the CO2 absorbent 13C supplied to the CO2 absorbent regenerator 15, the CO2 absorption rate of the flue gas 11B of the lower CO2 absorption unit 141A can be increased. Accordingly, since the CO2 recovery unit 1 has an excellent CO2 absorption rate even when the synthetic gas having a high CO2 partial pressure in the flue gas 11B is treated, energy can be saved.

Additionally, in the above-described embodiment, an example of treating the flue gas 11A such as a synthetic gas containing CO2 discharged from a direct reducing furnace has been described, but the invention can be applied to various gases including a natural gas (a methane gas) containing CO2.

REFERENCE SIGNS LIST

    • 1, 2 CO2 Recovery Unit
    • 11A, 11B, 11C, 11D, 11E Flue Gas
    • 12 Cooling Tower
    • 121 Cooling Unit
    • 122 Heat Exchanger
    • 123 Circulation Pump
    • 124 Adjustment Value
    • 13 CO2 Absorbent (Lean Solution)
    • 13A CO2 Absorbent
    • 13B CO2 Absorbent (Semi-Rich Solution)
    • 13C CO2 Absorbent (Rich Solution)
    • 14 CO2 Absorber
    • 14a Tower Top Portion
    • 14b Tower Bottom Portion
    • 141 CO2 Absorption Unit
    • 142 Water Washing Unit
    • 143A Liquid Storage Unit
    • 143B Chimney Tray
    • 144A Liquid Storage Unit
    • 144B Chimney Tray
    • 145 Mist Eliminator
    • 15 CO2 Absorbent Regenerator
    • 15a Tower Top Portion
    • 151 CO2 Absorbent Supply Unit
    • 16 Flue Gas Duct
    • 21 Heat Exchanger
    • 22 Circulation Pump
    • 23 Adjustment Valve
    • 24 Heat Exchanger
    • 31 Regenerating Heater
    • 32 Adjustment Valve
    • 33 Circulation Pump
    • 41, 44 CO2 Gas
    • 42 Condenser
    • 43 Separation Drum
    • 45 Condensed Water Circulation Pump
    • 46, 47 Adjustment Valve
    • 50 Rich Solution Supply Pipe
    • 51 Rich Solution Pump
    • 52 Rich-Lean Solution Heat Exchanger
    • 53 Lean Solution Supply Pipe
    • 54 Lean Solution Pump
    • 55 Cooling Unit
    • 101 Control Device
    • 102 Thermometer (Temperature Measurement Device)
    • L1, L2, L4 Circulation Line
    • L3, L11 Extraction Line
    • L5 Gas Discharge Line
    • L6 Condensed Water Line
    • L12 Re-Circulation Line
    • S Saturation Steam
    • W1 Cooling Water
    • W2, W3 Washing Water
    • W4 Steam Condensed Water
    • W5 Condensed Water

Claims

1. A CO2 recovery method comprising:

obtaining a first CO2 absorbent by causing a CO2 containing gas to be treated to contact a CO2 absorbent in a first CO2 absorption unit of a CO2 absorber so that CO2 contained in the gas to be treated is absorbed to the CO2 absorbent and obtaining a second CO2 absorbent by causing the first CO2 absorbent to contact the CO2 containing gas to be treated in a second CO2 absorption unit of the CO2 absorber so that CO2 contained in the gas to be treated is absorbed to the first CO2 absorbent;
regenerating the CO2 absorbent by heating the second CO2 absorbent in a CO2 absorbent regenerator so that CO2 is discharged from the CO2 absorbent; and
measuring a temperature of the second CO2 absorbent supplied from the CO2 absorber to the CO2 absorbent regenerator and controlling a temperature of the first CO2 absorbent supplied to the second CO2 absorption unit based on the measured temperature of the second CO2 absorbent, wherein
controlling the temperature of the first CO2 absorbent supplied to the second CO2 absorption unit such that the measured temperature of the second CO2 absorbent is in a range of 62° C. to 67° C.,
wherein a CO2 partial pressure of the CO2 containing gas to be treated is in a range of 50 kPa to 200 kPa.

2. The CO2 recovery method according to claim 1,

wherein the temperature of the first CO2 absorbent supplied to the second CO2 absorption unit is controlled so that the temperature is in the range of 50° C. to 60° C.

3. The CO2 recovery method according to claim 1,

wherein a ratio (the first CO2 absorption unit:the second CO2 absorption unit) between a filling material charging height in the first CO2 absorption unit and a filling material charging height in the second CO2 absorption unit is in the range of 1:3 to 3:1.
Referenced Cited
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20130333559 December 19, 2013 Nakagawa
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Foreign Patent Documents
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Patent History
Patent number: 10449481
Type: Grant
Filed: Oct 7, 2014
Date of Patent: Oct 22, 2019
Patent Publication Number: 20160361682
Assignee: MITSUBISHI HEAVY INDUSTRIES ENGINEERING, LTD. (Kanagawa)
Inventors: Atsuhiro Yukumoto (Tokyo), Takuya Hirata (Tokyo), Hiroshi Tanaka (Tokyo), Akiyori Hagimoto (Tokyo), Haruaki Hirayama (Tokyo), Tsuyoshi Oishi (Tokyo)
Primary Examiner: Cabrena Holecek
Application Number: 15/119,023
Classifications
Current U.S. Class: Amine (423/228)
International Classification: B01D 53/14 (20060101);